US2859256A - Separation process involving adsorption and desorption - Google Patents

Separation process involving adsorption and desorption Download PDF

Info

Publication number
US2859256A
US2859256A US484833A US48483355A US2859256A US 2859256 A US2859256 A US 2859256A US 484833 A US484833 A US 484833A US 48483355 A US48483355 A US 48483355A US 2859256 A US2859256 A US 2859256A
Authority
US
United States
Prior art keywords
straight chain
chain hydrocarbons
desorption
adsorption
adsorbent material
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US484833A
Inventor
Howard V Hess
Michael D Riordan
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Texaco Inc
Original Assignee
Texaco Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Texaco Inc filed Critical Texaco Inc
Priority to US484833A priority Critical patent/US2859256A/en
Application granted granted Critical
Publication of US2859256A publication Critical patent/US2859256A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
    • C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves

Definitions

  • This invention relates to a method of separating a mixture of organic compounds. More particularly this invention relates to a process for the separation of straight chain organic compounds, such as straight chain hydrocarbons, from a mixture containing the same together with non-straight chain organic compounds, such as nonstraight chain hydrocarbons, involvingadsorption of the straight chain organic compounds followed by desorption of the adsorbed straight chain organic compounds.
  • the practice of this invention is particularly applicable to the separation of straight chain hydrocarbons from a mixture containing the same such as a petroleum fraction, a synthetic .petroleum fraction, e. g. Fischer-Tropsch hydrocarbon synthesis fraction, a shale'oil fraction and thelike.
  • Still another object of this invention is, to provide a process for the selective adsorption of straight chain hydrocarbons from a mixture containing the same, involving isothermal adsorption and desorption operations.
  • Still another object of this invention is to provide a convenient method for effecting the desorption of straight chain hydrocarbons from an adsorbent material containing straight chain hydrocarbons adsorbedtherein.
  • an improved adsorption-desorption operation is effected, involving the separation of straight chain organic'compounds, such as straight chain hydrocarbons, from a mixture containing chain organic compounds from the adsorbent material by subjecting the adsorbent material containing adsorbed straight chain organic compounds to a relatively reduced pressure P P being greater than P
  • Any selective adsorbent material which selectively adsorbs straight chain organic compounds, such. as the straight chain hydrocarbons, to the substantial exclusion of non-straight chain organic compounds, such. as the non-straight chain hydrocarbons, is suitable in the practice of this invention.
  • straight chain organic compounds is meant any acyclic, straight chain organic compound which does' not evidence side chain branching.
  • straight chain organic compounds are the normal paraffins, e. g. n-butane, n-pentane and their higher molecular weight homologues, the n-butenes, the n-pentenes and their higher molecular weight homologues, the normal polyolefins, such as the butadiene s' and the normal acetylenic hydrocarbons, e. g. n-butyne.
  • nonstraight chain organic compounds is meant any aromatic, alicyclic or naphthenic, or acyclic or aliphatic compound which possess side chain branching.
  • molecular sieve that is, matter made up of porous crystals wherein the pores of the crystals are of molecular dimension and are of uniform size.
  • a particularly suitable solid adsorbent for straight chain organic compounds, such as straight chain-hydrocarbons is 'a calciutn alumino-silicate, apparently actually-fa sodiumeaL cium alumino-silicate manufactured by Lin'de Air-Products Company and] designated Linde Type 5A Molecular Sieve.
  • silicate have a pore size or diameter of about -'5 Angstrom units, a pore size sufiiciently'large to admit straight chain hydrocarbons, such as the normal paraffins, to the substantial exclusion of-the' non-straight chain naphthenic and aromatic and isoparafiinic and isoolefinic hydrocarbons.
  • This particular selective adsorbent - is available in various sizes such as A and /8" diameter pellets as well as in the form of a finely divided powder.
  • Suitable solid selective adsorbents include the synthetic and natural-zeolites, which, when dehydrated,
  • suitable-naturally occurring zeolite is analcite NaAlSi O ;H O V which, when dehydrated, when all or part of the sodium is replaced by *an alkaline earth metal, such as calcium,
  • selective adsorbents having the property of selectively adsorbing straight chain hydrocarbons over non-straight chain" hydrocarbons in the manner of a molecular sieve may he obtained by suitable treatment of various oxide gels,-especially metal oxide gels of the Other solid adsorbents'which selectively'adsorb straight chain hydrocarbons to the substantial exclusion of non-straight chain. hydrocarbons are also known.
  • the separation process in accordance with this invention calls for carrying out the adsorptive separation of the straight chain hydrocarbons at a relatively'elevate'd pressure P; followed by the desorption of the adsorbed straight chain hydrocarbons at a relatively reduced pressure P
  • Any relatively elevated adsorption pressure P may be employed in the practice of this invention.
  • adsorption pres is suitable.
  • the choice of adsorption pressure P is sometimes dependent upon the composition of the mixture undergoing separation or whether or not it is desired to carry out liquid phase adsorption or vapor phase adsorption.
  • any relatively reduced desorption pressure P may be employed in the practice of this invention provided, of course, P is less than P
  • the relationship or ratio of the adsorption pressure P, (absolute) to the desorption pressure P (absolute) as indicated by P /P is suitablyin the range 1.1-750.
  • the adsorption operation may be carried out -at any suitable' temperature depending to some extent upon-the composition of the mixture ;undergoing separation for The crystals of this particular calciumaluminoperatures may be employed in the practiceof this invention, the uppertemperature'limitation being governed by the temperaturestability of the selective adsorbent material, the temperature stability of the mixture undergoing separation and the temperature stability of the adsorbed-desorbed straight chain organic compounds.
  • the adsorption operation may be carried out in either the liquid phase or the-vapor phase. It is preferred, however, to carry out the desorption operation in the vapor phase, that is, during thedesorption operation it is preferred to adjust the temperature and pressure thereof with respect to the straight chain organic compounds being desorbed such that the desorbed straight chain organic compounds are in the vapor phase;
  • the adsorptiontemperature is preferably substantially above the normal atmospheric boiling point of the straight 'chain'organic compounds in the mixture undergoing separation and preferably also above the normal atmospheric boiling point of the'mix- 'ture undergoing separation.
  • the remaining liquid phase now having a substantially reduced amount of straight chain organiccom- I pounds, is separated from the adsorbent, while still maintaining the relatively elevated adsorption pressure.
  • the adsorbent material is subjected to a rela-v tively'reduced desorption pressure with the result that the absorbed straight chain organic compounds are flashed-off or desorbed from the'adsorbent under substantially isothermal conditions.
  • the heat or desorption will cause some temperature decrease or cooling of the adsorbent during the desorption operation with the result that strictly isothermal adsorption-desorption operations may not be possible without theaddition of heat to the adsorbent material during the desorption operation.
  • the cooling eifect of the heat of desorption can, however, be counteracted or compensated for during the desorption operation by contacting or passing through the adsorbent material a hot gaseous stripping medium -at a sufficient temperature to supply the heat of desorption and thereby maintain the desorption operation at substantially the same temperature as the adsorption operation.
  • Any suitable inert gaseous stripping medium maybe employed to supply the heat of desorption.
  • the molecular dimensions of the stripping medium or agent permit it to enter the pores of the selective adsorbent and thereby aid in displacing the adsorbed straight chain organic compounds therefrom.
  • Typical suitable inert gaseous stripping agents include nitrogen, flue gas, carbon dioxide, methane, hydrogen, the monatomic gases, natural gas, steam or superheated steam and the like.
  • the treated mixture is displaced or separated from contact with the adsorbent material by means of a gaseous, inert, displacing medium.
  • the pressure exerted upon. the adsorbent material in the system is then reduced with'the result that the adsorbed straight chain organic compounds are released or tend to be released fromthe adsorbent material.
  • Straight chain hydrocarbon-containing mixtures which are suitably treated in accordance with this invention for the separation of the straight chain hydrocarbons therefrom include the various petroleum fractions such as naphtha fraction, a kerosene fraction, a diesel oil fraction, a gas oil fraction and the like.
  • Particularly suitable for treatment in accordance with this invention are straight chain hyrocarbon-containing fractions having a boiling point or boiling range in the range of 40600 F. and containing at least a substantial amount of straight chain hydrocarbons, e. g. 2-35 by volume and higher.
  • the following examples are'illustrative of the practice of this invention.
  • the recovered upgraded gasoline or eflluent amounted to 84.8% by volume
  • the adsorbed straight chain hydrocarbons were desorbed from the adsorbent material at a temperature of 425 F. and at an absolute pressure of 40 mm. Hg.
  • the desorption of the straight chain hydrocarbons from the adsorbent material was aided by the injection of a stream of nitrogen during the desorption operation so as to sweep out the desorbed straight chain hydrocarbons from the adsorbent material and from the vessel containing the adsorbent.
  • EXAMPLE 2 A number of runs were carried out at a relatively elevated temperature and pressure in order to eflFect vapor phase selective adsorption of straight chain hydrocarbons from an aviation gasoline base stock, followed by desorption at substantially atmospheric pressure. These runs were carried out as follows. The vessel containing a fixed bed of selective adsorbent (Linde Type 5A Molecular Sieve) was pressured to the desired adsorption pressure by means of a gas, such as nitrogen. After the vessel had been brought up to the desired adsorption temperature and pressure, the vaporized mixture or charge stock to be upgraded by separation of the straight chain hydrocarbons therefrom was introduced thereinto.
  • a gas such as nitrogen
  • adsorbent material may be in the form of pellets, powder, beads, granules, etc. and employed in a fixed bed, moving bed, fluidized bed and concurrently or countercurrently contacted with the mixture undergoing separation. Any satisfactory throughput may be employed, e. g., in the range 0.2-20.0 volume liquid charge mixture per volume of adsorbent per hour.
  • the periods of adsorption and desorption may be equal or different depending upon the results desired, composition of charge mixture, extent of adsorptive separation desired and various economic factors.
  • a process for separatingstraight chain hydrocarbons from a mixture containing [the same together with non-straight chain hydrocarbons which comprises contacting said mixture in the vapor phase at an elevated temperature and pressurewith a. selective adsorbent which selectively absorbs straight'chain hydrocarbons to the substantial exclusion of nou-strai'g'ht-chain hydrocarbons to adsorb straight chain hydrocarbons therefrom toyield a gaseous treated efiiuent having a reduced amount of straight chain hydrocarbons, displacing said gaseous efliuent from said solid adsorbent material by means of a displacing medium and subjecting the resulting adsorbent material now substantially free of said efiluent to a reduced pressure while contacting said adsorbent material desorption operation is ,carriedout at a pressure less than V atmospheric- 3.
  • said adsorbent is an aluminofsilicate.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Description

sired operating adsorption temperature.
United States Patent SEPARATION PROCESS INVOLVING ABSORPTION AND DESORPTION Howard V. Hess, Glenham, and Michael D. Riordan, Fishkill, N. Y., assignors to The Texas Company, New York, N. Y., a corporation of Delaware No Drawing. Application January 28, 1955 Serial No. 484,833
Claims. (Cl. 260-676) This invention relates to a method of separating a mixture of organic compounds. More particularly this invention relates to a process for the separation of straight chain organic compounds, such as straight chain hydrocarbons, from a mixture containing the same together with non-straight chain organic compounds, such as nonstraight chain hydrocarbons, involvingadsorption of the straight chain organic compounds followed by desorption of the adsorbed straight chain organic compounds. In accordance with one embodiment the practice of this invention is particularly applicable to the separation of straight chain hydrocarbons from a mixture containing the same such as a petroleum fraction, a synthetic .petroleum fraction, e. g. Fischer-Tropsch hydrocarbon synthesis fraction, a shale'oil fraction and thelike.
A number of processes have recently been proposed for treating or upgrading a hydrocarbon-containing fraction, suchas a pertoleum fraction containing straight chain and non-straight chain hydrocarbons, by selectively adsorbing the straight chain hydrocarbons therefrom by means of an adsorbent which selectively adsorbs straight chain hydrocarbons to the substantial exclusion of the non-straight chain hydrocarbons. For example, in copending, co-assigned patent application Serial No. 478,- 426, filed December 29, 1954, there is disclosed a method ing the straight chain hydrocarbons therefrom. Similarly in patent application SerialNo. 483,998, filed January 25, 1955, there is disclosed a method for upgrading a catalytic reformer efiluent, such as a Platformate, by selectively adsorbing the straight chain hydrocarbons therefrom. In each of the above-identified patent applications H V. Hess, one of the co-inventors of the subject application, is a co-inventor.
Previously disclosed methods for treating a mixture of straight chain hydrocarbons and non-straight chain hydrocarbons, involving selective adsorption of the straight chain hydrocarbons, have involved isobaric'adsorption-desorption operations, that is, adsorption-desorption operations carried out at substantially the same absolute pressure. When operations involving adsorption and desorption of straight chain hydrocarbons are carried out at substantially the same pressure it has been a practice to carry out the desorption operation at an elevated temperature, higher than the adsorption temperature, so that the adsorbed straight chain hydrocarbons may be more quickly desorbed from the adsorbent. Accordingly a desorption temperature substantially greater, for example l00-400 F. higher than the adsorption temperature, has been employed. Following the high temperature desorption operation, indicated above, the resulting desorbed-regenerated adsorbent must be cooled to the de- This cooling of the hot desorbed-regenerated adsorbent is time consuming and expensive. Moreover, it is obvious that the time required'to efiect cooling of the hot desorbedregenerated I 2,859,256 Patented Nov. 4, 1958 ice stricts the throughput or capacity of the adsorptive separation process.
It is an object of this invention to increase the rate at which adsorbed straight chain organic compounds can ,followed by desorption of the adsorbed straight chain hydrocarbons.
It is another object of this invention to provide a process for the adsorptive separation of straight chain hydrocarbons from a mixture containing the same to.- gether with non-straight chain hydrocarbons whereby an increased rate of desorption of the adsorbed straight chain hydrocarbons from the adsorbent material is possible.
Still another object of this invention is, to provide a process for the selective adsorption of straight chain hydrocarbons from a mixture containing the same, involving isothermal adsorption and desorption operations.
Still another object of this invention is to provide a convenient method for effecting the desorption of straight chain hydrocarbons from an adsorbent material containing straight chain hydrocarbons adsorbedtherein.
How these and other objects of this invention are accomplished will become apparent in the light of the accompanying disclosure. In at least one embodiment of this invention at least one of the foregoing objects will be achieved. f
In accordance with our invention an improved adsorption-desorption operation is effected, involving the separation of straight chain organic'compounds, such as straight chain hydrocarbons, from a mixture containing chain organic compounds from the adsorbent material by subjecting the adsorbent material containing adsorbed straight chain organic compounds to a relatively reduced pressure P P being greater than P Any selective adsorbent material which selectively adsorbs straight chain organic compounds, such. as the straight chain hydrocarbons, to the substantial exclusion of non-straight chain organic compounds, such. as the non-straight chain hydrocarbons, is suitable in the practice of this invention. By straight chain organic compounds is meant any acyclic, straight chain organic compound which does' not evidence side chain branching.
Examples of straight chain organic compoundsare the normal paraffins, e. g. n-butane, n-pentane and their higher molecular weight homologues, the n-butenes, the n-pentenes and their higher molecular weight homologues, the normal polyolefins, such as the butadiene s' and the normal acetylenic hydrocarbons, e. g. n-butyne. By nonstraight chain organic compounds is meant any aromatic, alicyclic or naphthenic, or acyclic or aliphatic compound which possess side chain branching. Examples'of non- In the practice of this invention it is preferred to ernployas the selective adsorbent material certain natural ,orsynthetic zeolites or alumino-silicates, such asacalcium alumino silicate, which exhibit the properties of a polyvalent amphoteric metal oxides.
sure in the range 10,000 p. s. i. g.
molecular sieve, that is, matter made up of porous crystals wherein the pores of the crystals are of molecular dimension and are of uniform size. A particularly suitable solid adsorbent for straight chain organic compounds, such as straight chain-hydrocarbons is 'a calciutn alumino-silicate, apparently actually-fa sodiumeaL cium alumino-silicate manufactured by Lin'de Air-Products Company and] designated Linde Type 5A Molecular Sieve. silicate have a pore size or diameter of about -'5 Angstrom units, a pore size sufiiciently'large to admit straight chain hydrocarbons, such as the normal paraffins, to the substantial exclusion of-the' non-straight chain naphthenic and aromatic and isoparafiinic and isoolefinic hydrocarbons. This particular selective adsorbent -is available in various sizes such as A and /8" diameter pellets as well as in the form of a finely divided powder.
Other suitable solid selective adsorbents include the synthetic and natural-zeolites, which, when dehydrated,
suitable-naturally occurring zeolite is analcite NaAlSi O ;H O V which, when dehydrated, when all or part of the sodium is replaced by *an alkaline earth metal, such as calcium,
by base 'exchange yields a material which may be represented .by the formula (Ca,Na )Al Si O .2H O and which, after "suitable conditioning, will adsorb straight 'chainhydrocarbons to the substantial exclusion of nonstraight chainhydrocarbons. Naturally occurring or synthetically prepared phacolite, gmelinite, harmotome and -the like or suitable base exchange'modifications of these are also suitable.
Other'solid selective adsorbents may be employed in the practice of'thisiinvention. For example, it is'contemplated that selective adsorbents having the property of selectively adsorbing straight chain hydrocarbons over non-straight chain" hydrocarbons in the manner of a molecular sieve may he obtained by suitable treatment of various oxide gels,-especially metal oxide gels of the Other solid adsorbents'which selectively'adsorb straight chain hydrocarbons to the substantial exclusion of non-straight chain. hydrocarbons are also known.
Described more particularly, the separation process in accordance with this invention calls for carrying out the adsorptive separation of the straight chain hydrocarbons at a relatively'elevate'd pressure P; followed by the desorption of the adsorbed straight chain hydrocarbons at a relatively reduced pressure P Any relatively elevated adsorption pressure P may be employed in the practice of this invention. Usually an adsorption presis suitable. The choice of adsorption pressure P is sometimes dependent upon the composition of the mixture undergoing separation or whether or not it is desired to carry out liquid phase adsorption or vapor phase adsorption.
Furthermore, any relatively reduced desorption pressure P may be employed in the practice of this invention provided, of course, P is less than P The relationship or ratio of the adsorption pressure P, (absolute) to the desorption pressure P (absolute) as indicated by P /P is suitablyin the range 1.1-750. have been carried out'wher'ein the ratio was not greater Satisfactory operations The adsorption operation may be carried out -at any suitable' temperature depending to some extent upon-the composition of the mixture ;undergoing separation for The crystals of this particular calciumaluminoperatures may be employed in the practiceof this invention, the uppertemperature'limitation being governed by the temperaturestability of the selective adsorbent material, the temperature stability of the mixture undergoing separation and the temperature stability of the adsorbed-desorbed straight chain organic compounds.
When a calcium alumino-silicate, such as Lin'de Type 5A Molecular Sieve, is employed as the selective adsorbent theadsorption and/ or desorption temperature should not -exceed:about 1300 F. since a temperature above about "l300 causes destruction of the adsorbent material, presumably by collapse of the crystal structure.
As indicated hereinabove, the adsorption operation may be carried out in either the liquid phase or the-vapor phase. It is preferred, however, to carry out the desorption operation in the vapor phase, that is, during thedesorption operation it is preferred to adjust the temperature and pressure thereof with respect to the straight chain organic compounds being desorbed such that the desorbed straight chain organic compounds are in the vapor phase;
temperature and pressure,'the adsorptiontemperature is preferably substantially above the normal atmospheric boiling point of the straight 'chain'organic compounds in the mixture undergoing separation and preferably also above the normal atmospheric boiling point of the'mix- 'ture undergoing separation. Following the adsorption operation the remaining liquid phase, now having a substantially reduced amount of straight chain organiccom- I pounds, is separated from the adsorbent, while still maintaining the relatively elevated adsorption pressure. Subsequently the adsorbent materialis subjected to a rela-v tively'reduced desorption pressure with the result that the absorbed straight chain organic compounds are flashed-off or desorbed from the'adsorbent under substantially isothermal conditions. It is realized that the heat or desorption will cause some temperature decrease or cooling of the adsorbent during the desorption operation with the result that strictly isothermal adsorption-desorption operations may not be possible without theaddition of heat to the adsorbent material during the desorption operation. The cooling eifect of the heat of desorption can, however, be counteracted or compensated for during the desorption operation by contacting or passing through the adsorbent material a hot gaseous stripping medium -at a sufficient temperature to supply the heat of desorption and thereby maintain the desorption operation at substantially the same temperature as the adsorption operation. Any suitable inert gaseous stripping medium maybe employed to supply the heat of desorption. Preferably the molecular dimensions of the stripping medium or agent permit it to enter the pores of the selective adsorbent and thereby aid in displacing the adsorbed straight chain organic compounds therefrom.
Typical suitable inert gaseous stripping agents include nitrogen, flue gas, carbon dioxide, methane, hydrogen, the monatomic gases, natural gas, steam or superheated steam and the like.
During the vapor phase adsorption-desorption substantially the same operations described hereinabove with respect to liquid phase adsorption are employed. More particularly 'after' theselective adsorbent'has beensub- In a liquid phase adsorption operation at an elevated of the feed charge.
stantially saturated with respect to straight chain organic compounds or after the straight chain organic com pounds have been removed to the desired extent from the mixture undergoing separation, the treated mixture is displaced or separated from contact with the adsorbent material by means of a gaseous, inert, displacing medium. The pressure exerted upon. the adsorbent material in the system is then reduced with'the result that the adsorbed straight chain organic compounds are released or tend to be released fromthe adsorbent material.
.The practice of this invention is particularly applicable to the separation of straight chain hydrocarbons from mixtures containing the same together with non-straight chain hydrocarbons. Straight chain hydrocarbon-containing mixtures which are suitably treated in accordance with this invention for the separation of the straight chain hydrocarbons therefrom include the various petroleum fractions such as naphtha fraction, a kerosene fraction, a diesel oil fraction, a gas oil fraction and the like. Particularly suitable for treatment in accordance with this invention are straight chain hyrocarbon-containing fractions having a boiling point or boiling range in the range of 40600 F. and containing at least a substantial amount of straight chain hydrocarbons, e. g. 2-35 by volume and higher. The following examples are'illustrative of the practice of this invention.
EXAMPLE 1 A columnar, fixed bed of selective adsorbent comprising 1067 grams of A pellets of a calcium aluminosilicate (Linde Type A Molecular Sieve) was contacted at a temperature of 425 F. with a vaporized catalytic reformed. gasoline, namely a Platformate, having an octane number of 80, at substantially atmospheric pressure and at a space velocity of about 1 v./hr./v. There was recovered as a vaporous efiluent an upgraded gasoline product having a reduced amount of straight chain hydrocarbons, in fact an ungraded gasoline substantially free of straight chain hydrocarbons and exhibiting and octane number CFRR Micro-clear of 89.3. The recovered upgraded gasoline or eflluent amounted to 84.8% by volume The adsorbed straight chain hydrocarbons were desorbed from the adsorbent material at a temperature of 425 F. and at an absolute pressure of 40 mm. Hg. The desorption of the straight chain hydrocarbons from the adsorbent material was aided by the injection of a stream of nitrogen during the desorption operation so as to sweep out the desorbed straight chain hydrocarbons from the adsorbent material and from the vessel containing the adsorbent. There was recovered a fraction containing substantially only straight chain hydrocarbons in an amount equal to 15.2% by volume of the charge.
EXAMPLE 2 A number of runs were carried out at a relatively elevated temperature and pressure in order to eflFect vapor phase selective adsorption of straight chain hydrocarbons from an aviation gasoline base stock, followed by desorption at substantially atmospheric pressure. These runs were carried out as follows. The vessel containing a fixed bed of selective adsorbent (Linde Type 5A Molecular Sieve) was pressured to the desired adsorption pressure by means of a gas, such as nitrogen. After the vessel had been brought up to the desired adsorption temperature and pressure, the vaporized mixture or charge stock to be upgraded by separation of the straight chain hydrocarbons therefrom was introduced thereinto. After a period of time, usually when the selective adsorbent was substantially saturated with respect to straight chain hydrocarbons the injection of vaporized charge stock thereinto was discontinued and the introduction of a gaseous displacing medium was started in order to sweep out or displace any of the gaseous treated charge stock from the adsorption vessel. Introduction of a gaseous sweeping oi displacing medium is advantageous when it is desired to obtain a desorbate containing substantially only straight chain hydrocarbons and/or a treated charge stock substantially free ofstraight chain hydrocarbons. After substantially all of the treated charge stock was displaced from the adsorption vessel, the pressure in'the-adsorption vessel was reduced to a'suit' able low value with the result that the adsorbed straight chain hydrocarbons were desorbed from the'adsorbent material. The desorption of the straight chain'hydrocarbons from the adsorbent material was aided by the continued injection of methaneas the displacing or stripping mediiim during" the desorption operation which was carried out at substantially atmospheric pressure and at a temperature of about 700 F. Thedesorp'tionbperation was carried out until substantially all of the straight chain hydrocarbonswere' desorbed. The resultof these operations are set forthfin the accompanying Tables I and II. I
Table I SELECTIVE FINISHING OF AVIATIONIBASE STOCK 92.2 CLEAR CFRR: at HOUR ABSORPTION. PERIOD THROUGHPUT1 V./V./HB..
, 4 Average Average Adsorption Average "CFRR RunNo. Adsorption Pressure, RI for 1st Clear 0c- Tempera p. a. i. g. 550 cc. tane No. ture, F: 4 Product for 1st 550 ccrEst'.
Table II SELECTIVE FINISHING OF A CATALYTIC -REFORMED AVIATION BASE STOCK HOUR ADSORPTION PERIOD THROUGHPUT 1 V./V./HR.
Average Avg. Adsorption Adsorption Average CFRR Run N0. Temp., Pressure, RI for 1st Octane N 0.
F. p. s. l. g. 365 00. for 1st 365 cc. Est.
501 200 1. 4555 97. 8 631 200 1. 4571 98. 6 526 350 l. 4562 98. l. 696 350 1. 4565 98. 2 508 500 1. 4559 98. 0 614 500 1. 4576 98. 8 721 500 l. 4560 98. 0 514 600 1.4574 98. 7 613 600 1. 4573 9S. 6 714 600 1. 4561 98. 1
To eflect adsorption of the straight chain organic compounds any suitable or conventional means or method for effecting liquid-solid or gas-solid contact may be employed. The adsorbent material may be in the form of pellets, powder, beads, granules, etc. and employed in a fixed bed, moving bed, fluidized bed and concurrently or countercurrently contacted with the mixture undergoing separation. Any satisfactory throughput may be employed, e. g., in the range 0.2-20.0 volume liquid charge mixture per volume of adsorbent per hour. The periods of adsorption and desorption may be equal or different depending upon the results desired, composition of charge mixture, extent of adsorptive separation desired and various economic factors.
Although the practice of this invention has been described hereinabove with reference to the separation of straight chain hydrocarbons from non-straight chain hydrocarbons it is apparent, in view of the accompanying disclosure, that the invention is also applicable to the separation of other compounds such as the separation oi straight chain alcohols from non-straight chain alcohols, more particularly the separation of iso-, secondary, and tertiary alcohols. By employingthe practice of thisin- Vention-n-propanol, n-butanol, n-pentanol, n-hexanol, nheptanol, n-octanoL'n-nonanol, n'-de canol and their higher molecular weight homologs maybe separated from their corresponding non-straight chain isomers or non-terminal hydroiry (0H) substituted isomers, such as the correspending 'iso-, secondary, andtertiary alcohols. i As will be apparent to'th'os'e ,skilled in the art upon readingthe foregoing. disclosure many modifications, substitutions and changes are .possible in the practice of this'invention without departing from the spirit or scope thereof.
we claim: I
1. A process for separatingstraight chain hydrocarbons from a mixture containing [the same together with non-straight chain hydrocarbons which comprises contacting said mixture in the vapor phase at an elevated temperature and pressurewith a. selective adsorbent which selectively absorbs straight'chain hydrocarbons to the substantial exclusion of nou-strai'g'ht-chain hydrocarbons to adsorb straight chain hydrocarbons therefrom toyield a gaseous treated efiiuent having a reduced amount of straight chain hydrocarbons, displacing said gaseous efliuent from said solid adsorbent material by means of a displacing medium and subjecting the resulting adsorbent material now substantially free of said efiluent to a reduced pressure while contacting said adsorbent material desorption operation is ,carriedout at a pressure less than V atmospheric- 3. A method in'accordance with claim 1 wherein, said adsorbent is an aluminofsilicate.
4. A method inaccordance with claim 1 wherein said displacing, medium is a normally gaseous hydrocarbon.
5. A method in accordance with claim 1 wherein said displacing medium and said gaseous stripping medium are the same material. a r v References-Cited inthe. file of this patent H UNITED STATES PATENTS 1,453,215 Voresset-al. Apr. 24, 1923 2,306,610 Barrer Dec. 29., 1942 2,376,425 Frey May 22, 1945 2,390,536 Houdry et a1. Dec. 11, 1945 2,425,535 Hibshman Aug. 12, 1947 2,442,191 Black May 25, 1948 2,449,402 Lipkin Sept. 14,1948 2,586,889 Vesterdalet. a1 Feb. 26, 1952 I-Iibshma'n Dec. 2, 1952

Claims (1)

1. A PROCESS FOR SEPARATING STRAIGHT CHAIN HYDROCARBONS FROM A MIXTURE CONTAINING THE SAME TOGETHER WITH NON-STRAIGHT CHAIN HYDROCARBONS WHICH COMPRISES CONTACTING SAID MIXTURE IN THE VAPOR PHASE AT AN ELEVATED TEMPERATURE AND PRESSURE WITH A SELECTIVE ADSORBENT WHICH SELECTIVELY ABSORBS STRAIGHT CHAIN HYDROCARBONS TO THE SUBSTANTIAL EXCLUSION OF NON-STRAIGHT CHAIN HYDROCARBONS TO ADSORB STRAIGHT CHAIN HYDROCARBONS THEREFROM TO YIELD A GASEOUS TREATED EFFLUENT HAVING A REDUCED AMOUNT OF STRAIGHT CHAIN HYDROCARBONS, DISPLACING SAID GASEOUS EFFLUENT FROM SAID SOLID ADSORBENT MATERIAL BY MEANS OF A DISPLACING MEDIUM AND SUBJECTING THE RESULTING ADSORBENT MATERIAL NOW SUBSTANTIALLY FREE OF SAID EFFLUENT TO A REDUCED PRESSURE WHILE CONTACTING SAID ADSORBENT MATERIAL WITH A GASEOUS STRIPPING MEDIUM AT A SUITABLE ELEVATED TEMPERATURE TO DESORB THE ADSORBED STRAIGHT CHAIN HYDROCARBONS THEREFROM AND TO MAINTAIN THE DESORPTION OPERATION AT SUBSTANTIALLY THE SAME TEMPERATURE AS THE ADSORPTION OPERATION, THE RESULTING DESORBED STRAIGHT CHAIN HYDROCARBONS BEING IN THE GASEOUS PHASE.
US484833A 1955-01-28 1955-01-28 Separation process involving adsorption and desorption Expired - Lifetime US2859256A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US484833A US2859256A (en) 1955-01-28 1955-01-28 Separation process involving adsorption and desorption

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US484833A US2859256A (en) 1955-01-28 1955-01-28 Separation process involving adsorption and desorption

Publications (1)

Publication Number Publication Date
US2859256A true US2859256A (en) 1958-11-04

Family

ID=23925807

Family Applications (1)

Application Number Title Priority Date Filing Date
US484833A Expired - Lifetime US2859256A (en) 1955-01-28 1955-01-28 Separation process involving adsorption and desorption

Country Status (1)

Country Link
US (1) US2859256A (en)

Cited By (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2920037A (en) * 1956-03-01 1960-01-05 Universal Oil Prod Co Separation of normal paraffins from hydrocarbon mixtures using zeolitic molecular sieves
US2944092A (en) * 1956-12-05 1960-07-05 Exxon Research Engineering Co Gasoline hydrocarbon separation recovery process using zeolitic molecular sieves
US2952630A (en) * 1956-11-19 1960-09-13 Shell Oil Co Separation of hydrocarbons using zeolitic molecular sieves
US2958714A (en) * 1956-08-31 1960-11-01 Exxon Research Engineering Co Adsorption process
US2966531A (en) * 1958-04-01 1960-12-27 Exxon Research Engineering Co Increasing efficiency of hydrocarbon separation with adsorbents
US2984620A (en) * 1957-08-01 1961-05-16 Union Oil Co Isothermal adsorption process for separation of organic nitrogen compounds from hydrocarbons
US2988502A (en) * 1957-04-26 1961-06-13 Exxon Research Engineering Co High efficiency hydrocarbon separation process employing molecular sieve adsorbents
US2988577A (en) * 1957-04-11 1961-06-13 Texaco Inc Selective sorption process
US2996558A (en) * 1957-04-17 1961-08-15 Exxon Research Engineering Co Molecular sieve separation process
US3007980A (en) * 1958-06-20 1961-11-07 Sun Oil Co Removal of impurities from volatile liquids
US3007545A (en) * 1955-12-21 1961-11-07 Exxon Research Engineering Co Method of extracting hydrocarbons
US3014078A (en) * 1959-02-02 1961-12-19 Union Oil Co Separation of cresol isomers
US3053913A (en) * 1959-01-21 1962-09-11 Gulf Research Development Co Separation of high molecular weight hydrocarbons with molecular sieves
US3054838A (en) * 1958-09-08 1962-09-18 California Research Corp Method for separating n-hydrocarbons using molecular sieves
US3069349A (en) * 1958-06-16 1962-12-18 Union Oil Co Hydrocarbon isomerization process
US3090748A (en) * 1959-11-17 1963-05-21 Exxon Research Engineering Co Process for desulfurization employing a nitrile impregnated substrate
US3121625A (en) * 1960-10-05 1964-02-18 Universal Oil Prod Co Adsorptive separation of gas mixtures
US3140322A (en) * 1958-08-14 1964-07-07 Socony Mobil Oil Co Inc Selective catalytic conversion
US3182017A (en) * 1963-04-05 1965-05-04 Union Oil Co Separation of naphthenes from hydrocarbon mixtures using 7 a. to 12 a. molecular sieves
US3183182A (en) * 1961-09-08 1965-05-11 British Petroleum Co Prolongation of sieve capacity by controlled desulfurization
US3184406A (en) * 1961-11-03 1965-05-18 British Petroleum Co Separation processes
US3226914A (en) * 1962-09-04 1966-01-04 Union Carbide Corp Pressure cycle for molecular sieve separation of normal paraffins from hydrocarbon mixtures
US3231631A (en) * 1962-01-19 1966-01-25 British Petroleum Co Separation process
US3244619A (en) * 1964-02-10 1966-04-05 Texaco Inc Separation process
US3258417A (en) * 1959-01-02 1966-06-28 Texaco Inc Dewaxing by contact with a molecular sieve adsorbent
US3268440A (en) * 1959-04-13 1966-08-23 Union Carbide Corp Pressure cycle for molecular sieve separation of normal paraffins from hydrocarbon mixtures
US3271464A (en) * 1961-06-19 1966-09-06 Exxon Research Engineering Co Selective dehydration of secondary alcohol over 5-a sieve
US3287432A (en) * 1957-04-11 1966-11-22 Texaco Inc Selective sorption process
US3538168A (en) * 1969-06-02 1970-11-03 Atlantic Richfield Co Restoring or preserving metal alkoxides
US4394254A (en) * 1982-04-26 1983-07-19 Texaco Inc. Method for separating straight chain hydrocarbons using zeolites having large crystals
US11313649B1 (en) 2020-07-31 2022-04-26 Ryan Johnson Elevation range meter and method of ranging a target using said elevation range meter

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1453215A (en) * 1922-02-18 1923-04-24 Gasoline Recovery Corp Method of volatilizing, distilling, or separating absorbed vapors
US2306610A (en) * 1941-02-24 1942-12-29 Barrer Richard Maling Fractionation of mixtures of hydrocarbons
US2376425A (en) * 1941-06-02 1945-05-22 Phillips Petroleum Co Diolefin production
US2390536A (en) * 1942-07-07 1945-12-11 Houdry Process Corp Separation of hydrocarbon gases
US2425535A (en) * 1945-07-25 1947-08-12 Standard Oil Dev Co Separation of normal paraffins from iso-paraffins by means of activated cocoanut charcoal
US2442191A (en) * 1944-05-26 1948-05-25 Standard Oil Dev Co Synthetic adsorbent for separating hydrocarbons
US2449402A (en) * 1944-01-24 1948-09-14 Sun Oil Co Process for separating aromatic hydrocarbons from a hydrocarbon mixture
US2586889A (en) * 1949-08-23 1952-02-26 Standard Oil Dev Co Separation of straight-chain from branched-chain hydrocarbons
US2620363A (en) * 1950-09-29 1952-12-02 Standard Oil Dev Co Method of separating normal paraffins from isoparaffins by a solid adsorption process

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1453215A (en) * 1922-02-18 1923-04-24 Gasoline Recovery Corp Method of volatilizing, distilling, or separating absorbed vapors
US2306610A (en) * 1941-02-24 1942-12-29 Barrer Richard Maling Fractionation of mixtures of hydrocarbons
US2376425A (en) * 1941-06-02 1945-05-22 Phillips Petroleum Co Diolefin production
US2390536A (en) * 1942-07-07 1945-12-11 Houdry Process Corp Separation of hydrocarbon gases
US2449402A (en) * 1944-01-24 1948-09-14 Sun Oil Co Process for separating aromatic hydrocarbons from a hydrocarbon mixture
US2442191A (en) * 1944-05-26 1948-05-25 Standard Oil Dev Co Synthetic adsorbent for separating hydrocarbons
US2425535A (en) * 1945-07-25 1947-08-12 Standard Oil Dev Co Separation of normal paraffins from iso-paraffins by means of activated cocoanut charcoal
US2586889A (en) * 1949-08-23 1952-02-26 Standard Oil Dev Co Separation of straight-chain from branched-chain hydrocarbons
US2620363A (en) * 1950-09-29 1952-12-02 Standard Oil Dev Co Method of separating normal paraffins from isoparaffins by a solid adsorption process

Cited By (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3007545A (en) * 1955-12-21 1961-11-07 Exxon Research Engineering Co Method of extracting hydrocarbons
US2920037A (en) * 1956-03-01 1960-01-05 Universal Oil Prod Co Separation of normal paraffins from hydrocarbon mixtures using zeolitic molecular sieves
US2958714A (en) * 1956-08-31 1960-11-01 Exxon Research Engineering Co Adsorption process
US2952630A (en) * 1956-11-19 1960-09-13 Shell Oil Co Separation of hydrocarbons using zeolitic molecular sieves
US2944092A (en) * 1956-12-05 1960-07-05 Exxon Research Engineering Co Gasoline hydrocarbon separation recovery process using zeolitic molecular sieves
US2988577A (en) * 1957-04-11 1961-06-13 Texaco Inc Selective sorption process
US3287432A (en) * 1957-04-11 1966-11-22 Texaco Inc Selective sorption process
US2996558A (en) * 1957-04-17 1961-08-15 Exxon Research Engineering Co Molecular sieve separation process
US2988502A (en) * 1957-04-26 1961-06-13 Exxon Research Engineering Co High efficiency hydrocarbon separation process employing molecular sieve adsorbents
US2984620A (en) * 1957-08-01 1961-05-16 Union Oil Co Isothermal adsorption process for separation of organic nitrogen compounds from hydrocarbons
US2966531A (en) * 1958-04-01 1960-12-27 Exxon Research Engineering Co Increasing efficiency of hydrocarbon separation with adsorbents
US3069349A (en) * 1958-06-16 1962-12-18 Union Oil Co Hydrocarbon isomerization process
US3007980A (en) * 1958-06-20 1961-11-07 Sun Oil Co Removal of impurities from volatile liquids
US3140322A (en) * 1958-08-14 1964-07-07 Socony Mobil Oil Co Inc Selective catalytic conversion
US3054838A (en) * 1958-09-08 1962-09-18 California Research Corp Method for separating n-hydrocarbons using molecular sieves
US3258417A (en) * 1959-01-02 1966-06-28 Texaco Inc Dewaxing by contact with a molecular sieve adsorbent
US3053913A (en) * 1959-01-21 1962-09-11 Gulf Research Development Co Separation of high molecular weight hydrocarbons with molecular sieves
US3014078A (en) * 1959-02-02 1961-12-19 Union Oil Co Separation of cresol isomers
US3268440A (en) * 1959-04-13 1966-08-23 Union Carbide Corp Pressure cycle for molecular sieve separation of normal paraffins from hydrocarbon mixtures
US3090748A (en) * 1959-11-17 1963-05-21 Exxon Research Engineering Co Process for desulfurization employing a nitrile impregnated substrate
US3121625A (en) * 1960-10-05 1964-02-18 Universal Oil Prod Co Adsorptive separation of gas mixtures
US3271464A (en) * 1961-06-19 1966-09-06 Exxon Research Engineering Co Selective dehydration of secondary alcohol over 5-a sieve
US3183182A (en) * 1961-09-08 1965-05-11 British Petroleum Co Prolongation of sieve capacity by controlled desulfurization
US3184406A (en) * 1961-11-03 1965-05-18 British Petroleum Co Separation processes
US3231631A (en) * 1962-01-19 1966-01-25 British Petroleum Co Separation process
US3226914A (en) * 1962-09-04 1966-01-04 Union Carbide Corp Pressure cycle for molecular sieve separation of normal paraffins from hydrocarbon mixtures
US3182017A (en) * 1963-04-05 1965-05-04 Union Oil Co Separation of naphthenes from hydrocarbon mixtures using 7 a. to 12 a. molecular sieves
US3244619A (en) * 1964-02-10 1966-04-05 Texaco Inc Separation process
US3538168A (en) * 1969-06-02 1970-11-03 Atlantic Richfield Co Restoring or preserving metal alkoxides
US4394254A (en) * 1982-04-26 1983-07-19 Texaco Inc. Method for separating straight chain hydrocarbons using zeolites having large crystals
US11313649B1 (en) 2020-07-31 2022-04-26 Ryan Johnson Elevation range meter and method of ranging a target using said elevation range meter

Similar Documents

Publication Publication Date Title
US2859256A (en) Separation process involving adsorption and desorption
US2818455A (en) Desorption of straight chain hydrocarbons from selective adsorbents
US3039953A (en) Selective conversion of normal paraffins with a crystalline zeolite
US2818137A (en) Adsorptive separation process
US3188293A (en) Process for regenerating molecular sieves
US2859173A (en) Method of treating a petroleum fraction with molecular sieve adsorbents
US2891902A (en) Method of treating a petroleum fraction using selective solid adsorbents
US3226913A (en) Separation process
US2899379A (en) Desorption of zeolitic molecular sieves using ammonia
US2886508A (en) Method of treating a petroleum fraction using molecular sieve aluminosilicate selective adsorbents
US3658696A (en) Selected adsorption with a silanized crystalline alumino-silicate
US2894998A (en) Method of treating a c4 hydrocarbon stream
US3373103A (en) N-hydrocarbon separation with a molecular sieve
US2917449A (en) Method of upgrading a petroleum naphtha
US3309415A (en) n-paraffin separation process
US2920038A (en) Gasoline hydrocarbon separation recovery process utilizing molecular sieves
US2886509A (en) Naphtha treating process
US2944092A (en) Gasoline hydrocarbon separation recovery process using zeolitic molecular sieves
US3182017A (en) Separation of naphthenes from hydrocarbon mixtures using 7 a. to 12 a. molecular sieves
US2918511A (en) Isomerizing a c6 hydrocarbon fraction
US2957927A (en) Process for separating normal aliphatic hydrocarbons from hydrocarbon mixtures
US2935539A (en) Hydrocarbon separation process using metallic amine complex substituted molecular sieves
US3069349A (en) Hydrocarbon isomerization process
US2408950A (en) Treatment of hydrocarbons
US3342726A (en) Purging and desorbing a molecular sieve with pentane